Art of cracking hydrocarbon oils



May 14, 1935. H. 1.. PELZER ART OF CRACKING HYDROCARBON OILS Original Filed Feb. 19; 1929 4 Sheets-Sheet l INVENTOR Y v 1 i; M M- ATTORNEYS May 14, 1935. H, L, PELZER ART OF CRACKING HYDROCARBON OILS Original Filed Feb. 19, 1929 4 Sheets-Sheet 2 INVENTOR Harry 1.. P z r aELAM ATTOR N EY5 May 14, 1935.

H. L. PELZER 2,001,314

ART OF CRACKING HYDROCARBON OILS Original Filed Feb. 19, 1929 4 Sheets-Sheet 3 INVENTOR fl ir/7- L, Pe/zer BY ATTORNEYS May 14, 1935.

H. L. PELZER ART OF CRAQKING HYDROCARBON OILS Original Filed Feb. 19, 1929 4 sheets sheet 4 Mk QM.

INVENTORI //arr L. le/zer ATTORNEYS Patented May 14, 1935 2,001,314 ART or CRACKING HYDROCARBON OILS.

Harry L. Pelzer, Houston, Tex, vassignor to Sinclair Refining Company, New York, N. Y a.

corporation of Maine Original application February 19, 1929, Serial No. 341,215. Divided and this application February 27, 1981, Serial No. 518,722

4 Claims. (Cl. 196-'58) 5 The amount of sulphur may vary, for example,

from a fraction of one per cent to several per cent on the oil. Sometimes the sulphur is present in a form such that its removal offers no particular difficulties, sometimes in a very refractory form. The removal of sulphur or the conversion of sulphur to an unobjectionable form is one of the .importantpurposes of most refining treatments to which petroleum oil products are usually subjected. In this aspect the sulphur is objectionable because 'it impairs the quality of the product. Frequently the sulphur is objectionable in another aspect, namely as a cause of corrosion. Cracking operations as commonly carried out usually involve the mainte-v nance of high temperatures and high pressures, and in this latter aspect the presence of sulphur in stocks subjected to cracking operations consequently involves special difficulties because high temperatures tend to accelerate corrosion and high pressures increase the element of danger resulting from corrosion.

This invention relates to improvements in the cracking of heavy sulphur-containing hydrocarbon oils, such as gas oil, crude oil, topped crude oil, fuel oil, by distillation under superatmospheric pressure to produce lighter hydrocarbon oils, such as gasoline. This application is a division of my original application for United States Letters Patent Serial Number 341,215 filed February 19, 1929.

According to this invention, a desulphurizing agent is supplied to the cracking operation dis persed in raw oil supplied to the cracking'operation, or in that part of the raw oil supplied to the cracking operation more objectionable withrespect to corrosion. This raw oil including a dispersed desulphurizing agent is passed through a heating zone into a vaporizing zone from which vapors including vapors of the desired distillate product are taken ofi under superatmospheric pressure and oil free from suspended matter, reaction products of the desulphurization or unconsumed desulphurizing agent or pitch or pitch-like solids or semi-solids formed by the cracking reaction, from the vaporizing zone, is passed through a separate heating zone into the vaporizing zone. In the first mentioned, or primary, heating zone, the raw oil including a desulphurizing "agent is heated approximately to the temperature prevailing in the vaporizing zone or to a higher temperature, andwith advantage to a cracking temperature, and inthe second mentioned, or secondary, heating zone, oil free from suspended matter, from the vaporizing zone, is heated to a cracking temperature. Heat is, with advantage, supplied to both heating zones by the .same stream of heating gases, andthis stream of heating gases is, with advantage, passed first in heat exchange with the oil passing through the. primary heating zone and then in heat exchange with the oil passing through the secondary heatingzone, particularly where a relatively high velocity of fiowis maintained through the primary heating zone, as described below.--- i I The oil free from, suspended matter passed through the secondary heating zone may consist exclusively of condensed higher boiling constituents separated from the vapors taken off from the vaporizing zone or a mixture of such condensed higher .boiling constituents and raw oil, particularly raw oil less obiectionable with respect to corrosion, or the oil passed through the secondary heating zone may include unvaporized oil from the vaporizing zone from which suspended matter has been separated before it is recirculated through the secondary heating zone.

The :raw oil including a dispersed desulphurizing agent is, with advantage, preheated before it is supplied to the primary heating zone; It may, for example, be so preheated by'indirect heat exchange with the vapors taken off from the vaporizing zone and undergoing partial-condensation. It may, for example, be so preheated by direct heat exchange with the vapors taken res PATENT, OFF-ICE.

off from the vaporizing zone andanycondensate operation. The, raw oil including a'dispersed desulphurizing agent :may also,,for example, be preheated by heat exchange with waste heating gases .or in a separate heating furnace before being supplied to the primary heating zone,

The desulphurizing agents useful in carrying out this invention include lime, caustic alkali, alcoholic solutions of caustic alkali, copper oxide or copper silicate gels, finely divided absorbent materials such as fullers earth carrying dispersed copper salts such ascopper chloride. The invention is particularly adaptedto utilize finely divided solid desulphurizing agents supplied in suspension in raw oil. The invention is also adapted to utilize liquid or semi-liquid desulphurizing agents supplied in emulsion'in rawoil.

The invention has a number of advantages which will appear as the description proceeds.- In particular, the invention provides an advantageous method of combating corrosion in the it cracking of sulphur-containing hydrocarbon oils by distillation under superatmosphric"pressure" of apparatus.

Referring to the accompanying drawings, Fig. 1 represents a pressure still system adapted for carrying out the invention,'-Fig. 2 represents a modified pressure still systemcorresponding to Fig. 1, adapted for carrying out the invention,

Fig.- 3 is an enlarged but-fragmentary representation of a divided reflux tower, and Fig. 4 represents a further modified pressure still system,

corresponding to'Fig. 1, adaptedfor carrying out the invention.

The pressure still illustrated in-each of Figures 1, 2 and 4 comprisesavap'orizing drum I, a bat-' tery of heating tubes 2, the secondary heating Zone arranged in the heating flue of a heating 1 furnace '3, and another battery of heating tubes 4; the primary heating zone, arranged in the heating flue-of the heating furnace '3 in advance of the batteryof heating-itubesl Theheating furnace 3 comprises afirebox 5-c'ommu'nicating with the upper end of the heating flue'in'which the heating tubes are arrangedand a stack flue B communicating with the lowerend or this same heating flue. Blowers l are provided for recirculation through the heating flue of part of the escaping heating gases,as' described in United States Letters Patent Nos. 1,574,5516 and"1,574,547 granted February 23, 19 26, to the Sinclair Re fining Company on the'application of John E.- Bell. In a still system comprising a vaporizing drum I about 9 by 30", the battery of heating tubes 2 may comprise fifty 4" tubes 20' long connected in parallel and the batteryof heating tubes}; may comprise twenty-one 47 tubes 1Q' long connected in series. The ,exact' arrangement of the heating tubesjinthe secondary heating zone is not important; they may, 'for example, be arranged as illustratedland described in an ap-. plication filed June 7, 1927, Serial No. 197,035 by me, orthese heating'tubes, also may be connected in series or .in series connected groups. The exactar'rangement of the,- heating tubes in the primary heating zone also is not important; how: ever, the heating tubes in 'theprimary heating zone are with advantage arranged tormaintain a relatively high velocity of flow therethrough and in this respect it is advantageous to connect these heating tubesin series or in series connected groups.

Referring more particularly to Fig. 1, a reflux tower 8 is arranged above the vaporizing drum I. Vapors escape from the vaporizing drum I to the lower end of the reflux tower 8 through vapor line 9 and vapors remaining uncondensed escape from the upper end of the reflux tower 8 through vapor line ID to condenser I I. This condenser is arranged'to discharge into a receiver 52 from which the distillate product of the operation is discharged through connection I3, uncondensed.

vapors and gases escaping through connection I l. The pressure in the system may be maintained and regulated by means of valve l5 in the vapor line I between the reflux tower 8 and the condenser I I-or by means of suitable valves arranged beyond the condenser or receiver. Reflux condensate from thelower endv of the reflux tower 8 is discharged, through connection Ifia to a circulating pump, I'Ia, which then forces this oil mixture through connection i8upwardly through the heating tubes! through connection !8 to the vaporizing drum I. This oil mixture is heated to a' cracking temperature in the heating tubes ,2. The particular type of circulating pump i1 lustrated, is described in more detail in an application filed June, 17, 1927, SerialNo. 197,209

by Thomas de G. Tifft.

A tar line, 29a, is provided for discharging unvaporized oil from the vaporizing drum I during operation. Connection BI is provided for in; itially charging the still and for pumping out the still at the endfof a run. Connection 22 is provided for supplying cooling oi1;to the bearings of the circulating pump. Connection 23 is pro-' vided for introducing raw oil intothe uppzr end of the reflux tower'B in direct contact with the vapors therein, for examplefor'effecting orcontrolling the refluxing operation therein. 'Connections 24 and 25 are provided for. supplying the rawoil including a dispersed desulphurizing agent to the heating tubes 4. This raw oil, or part of, this raw oil, by means of thevalves shown, may be circulated through the coil 26 in indirect heat exchanging relation with the vapors in the reflux tower 8, for example for preheating this raw oil or for effecting or controlling the refluxing operation. V

Referringmore' particularly to Fig. 1, the provision of a closure valve 2'! in a pressure still of the type illustrated, and the particulartype of closure valve illustrated, is described in moredetail in an application filed January 12, 1923, Serial No. 246,263, by Eugene C. I-Ierthel; This closure valve 2! is used for bringing this still into' operation. ,To bring the pressure still illustrated in Fig.1 to operating conditions of temperature and pressure, the still is charged withenough oil to fillthefdrum I, say, one-third full, pump Ila is started to maintain circulation of the oil charge from the drum I through the heating tubes 2 back to the drum I, oil is forced, throughconnections Hand 25, through the heating tubes 4 intothe drum I,'fires are'started in the heating furnace 3, drips are taken 01f, valve I is then closed until the desired operating pressure is reached, valve 2] is then closed very gradually and valve I5 is gradually opened and regulated to maintain the desired operating pressure, any excess oil accumulating in the drum I during this period-being discharged through connectioniila.

In the type of'pressure still illustrated in Fig, 1, the oil passed through'the secondary heating zone, the battery of heating tubes 2, consists exclusively, during regular operation, of higher boiling constituents condensed in the reflux tower 8 from thejvapors taken ofi from the vaporizing drum l or a mixture of higher boiling constituents so condensed and raw oil supplied through connection 23. e 1 V For the production of gasoline from gas oil, for example, pressures in the neighborhood of 90-125 pounds per square inch may be employed, or higher pressures up to 300 pounds per square inch or more may be employed. In general,

higher pressures are employed with lower boiling charging stocks or to produce lower boiling distillate products. In any particular case the temperature will be determined by the pressure used.

The initial charge of oil may consist of the same stock to be supplied during operation'or, particularly if the stock to be supplied during operation contains a large amount of objectionable sulphur, the initial charge may consist of some other stock containing a relatively small amount of objectionable sulphur or, if the stock to be supplied during operation is a crude or topped crude or fuel oil or contains a large amount'of tarry or pitchy constituents, the initial charge may consist of a clean .gas oil stock. Similar stocks or different stocks may be supplied'to the battery of heating tubes making up the primary heating zone and to the battery of heating tubes been brought to operating conditions of temperature and pressure, the raw sulphur-containing stock with a desulphurizing agent dispersed therein is forced through the heating tubes 4 into the vaporizing drum I. For example, from A to' 4 pounds of hydrated lime may be dispersed in each barrel (42 gallons) of the raw sulphur containing stock supplied to the heating tubes 4.

Vapors including vapors of the desired distillate product and .vapors of constituents higher boiling than suitable as components of the desired distillate product are taken off from the vaporizing drum I under superatmospheric pressure to the reflux tower 8 in which higher boiling constituents are condensed. This condensation may be efiected or controlled, for example, by the circulation of the raw sulphur-containing stock on its way to the heating tubes 4, or part of this stock, through the coil 26 or by the introduction of raw oil through connection 23 or by both of these means conjointly. The condensate from the reflux tower 8, together with any admixed unvaporized raw oil supplied through connection 23, is circulated through the heating tubes 2 back to the vaporizing drum I. In the pressure still illustrated in Fig. l, the oil circulated through the heating tubes 2 consists exclusively either of reflux. condensate or of a mixture of reflux condensate and raw oil, this oil being free from suspended matter such as reaction products of the desulphurization or unconsumed desulphurizing agent or pitch or pitch-like solids or semisolids formed by the cracking reaction. In the pressure still illustrated .in Fig. 1 the residue including higher boiling constituents of the raw sulphur-containing stock supplied to the still, particularly where this stock is a crude or topped crude or-fuel oil, and solid or semisolid reaction products of the desulphurization reaction or the cracking reaction and any unconsumed desulphurizing agent is discharged, through connection 2011., without permitting circulation of any part of this residue through either heating zone.

In the pressure still illustrated in Fig. v1, no unvaporized oil from the vaporizing drum 1 is permitted to circulate, during regular operation, through either heating zone. through the'heating tubes 2 is heated to a cracking temperature therein. The oil passing'through the heating-tubes is, with advantage, heated approximately to the temperature prevailing in the vaporizing drum I or to a higher temperature, and the temperature towhich this oil is heated in the heating tubes 4 is, with advantage, a cracking'temperature. 'The condens- The oil passing ing operation effected in the reflux tower 8 is regulated to condense all constituents of the vapors. passing therethrough higher 'boilingthan Where-rawoil is supplied through connection 23 during regular operation,-the oil so supplied, for example, may be a clean gas oil stock or a stock sufliciently free from objectionable sulphur compounds to permitv its introduction in this manner without involving difiiculties due to corrosion.

In describing the apparatus illustrated in Figs. 2 to 4, any parts not specifically described in connection with these figures will be designated by the same reference numeral as the corresponding part in Fig. 1 and. the description of that part and of its relation to the still system maybe taken as thesame as for the corresponding part in Fig. 1. s a

Referring more particularlyto Fig. 2, a pair or reflux towers 29 and 30 are arranged above the vaporizing drum I. Vapors escape from the vaporizing drum l to the lower'end of the reflux tower 29 through vapor line 3!, from. the upper end of the reflux tower 29 to the lower end of the reflux tower 39 through vapor line 32 and from the upper end of the reflux tower 30 through vapor line 33, to condenser H as previously described in connection'with Fig. 1. The raw oil including a dispersed desulphurizing agent is introduced intothe upper end of reflux tower 29 in direct contact with the vapors therein through connection 34 and this raw oil together with higher boiling constituents condensed in the reflux tower 29 is forced, by means of pump 35, to and through the heating tubes 4, through connection 25. Part of the raw oil including a dispersed desulphurizing agent may be supplied directly to the heating tubes 4 through connection 36. The particular type of pump illustrated, designated 35, and also the pump designated 39, is described in more detail in applicationS-erial No. 197,209 mentioned above. The raw oil including a dispersed desulphurizing agent supplied to the heating tubes 4 either through connection 34 or through connection 36 may first be preheated, or

with the vapors i-n reflux tower .30. Inthe reflux towerifljconstituents higher boiling than suitable as components of thedesired distillateprgductand suitable to be supplied to the heating.

tubes 2 to be heated to a cracking temperature therein are condensed andsupplied to the heating tubes 2 either, through connection 31 by tion 40 and introduced into theupper'end of the refluxtoweraaitin direct contact with the vapors therein.v Anyunvaporized raw disc introduced into reflux tower 30 issupplied to the heating tubes 2 together with the condensate from the refluxtower 30 eitherthrough connec-- tion 31 or through connection 38.; This operation isadvantageous particularly where the raw stock containing objectionable'sulphur compounds is.

relatively more refractory. t

Instead of using a pair of reflux towers as illustrated in Fig. -2,-. a singledivided tower maybe usede mferring to Fig-3, for examplethe vapor line 3! from the vaporizing drum I may connect to the lower endnof the reflux tower M throughconnection 3i';;the vapor line 33 may connect to the upper'end of this reflux tower through connection-33f,condensate from the upper part of this, tower-may be withdrawn. by means of-panAZ and; supplied to pump Ila or pump 39 through connection 53, the raw oil including a .disperseddesulphurizing agent may be introduced into the lower part. of this tower through connection 54 and condensate from the lower. part ofthis tower together with unvaporizedr-aw oil supplied topump 35 throughconnection 55.. The refluxingoperation in the upper partoi the reflux'tower ll maybe effected or controlled, for example, by the'regulated introduction 'of'a refluxing medium through connection 36, and the refluxing operation in the lower part ofthis tower effected by the'introduction or raw oil through connection M may be supplemented or controlled by tl le regulated introduction of another refluxing medium through.

connection 11. Raw oil less objectionable with respect to corrosion, a clean gas oil' for example, may be supplied through connections 46 or 41 or both of these connections as'a refluxing medium or a stock "vaporizing substantially completely under the conditions ofgtemperature-and pressure prevailing in the refluxtowena part of the distillate product, for example, maybe supplied through connections AEior 41 or both of these connectionsas arefluxing medium. .It is. sometimes advantageous to supply raw oilto oe subjected to the cracking operation through connection 4i as a refluxing n ediuinand to supply a stock vaporizing substantially completely under the prevailing conditions of temperature and pressure through connection 46 a refluxing medium.

Referring more particularly to Fig. 4, a pair of reflux towers E5 and 49 are arranged above the vaporizing drum i.. Vapors escape from the vaporizing drum l to the lower end of the reflux tower 48 through vapor-line 5il,.from the upper end of the reflux tower '43 to the lower end of the reflux tower as, through vapor line 5| and from the upper end of the reflux tower 49 through vapor line 52 to the condenser 'i I. The raw oil including adispersed desulphurizing agent is introducedinto the upperend'of the reflux tower 49 indirect contact with the vapors therein throughconnection 53; and 'thisraw' oil together with higher boiling constituents J condensed in the reflux tower is forced,;-by n1eansof pump 54, to

and through'the heating tubes .4,'through connection 25. Part of the raw oil including a dis-.

persed desulphurizing agent; may be supplied directly to the heating tubes 4 throughconnection 55. The particular type ot ump illustrated designated 54; isdescribed in more detail in application Serial No.-197,2091mentioned above.

In the reflux tower 48, higher. boiling constituents are condensed and supplied to -the heating tubes '2 either through connection 56 bymeans of pump 39 or through connection 51 by means of pump Ha. For efiecting or controlling the refluxing operation in reflux towe1"48 raw*oil less objectionable with respect to corrosion fmaylbe. supplied through connection 58andintroduced into theupper endioftherefiux'tower lli in direct con-v tact. with the vaporslfiherein. Any unvaporized raw oil so. introduced into thereflux tower 48 is supplied tothe heating. tubes 2 together with the condensate; from the; reflux tower .48..-either through connection 56'onthrough connection 51. This operation is advantageous particularly where the raw stock containing objectionable sulphur compounds is relatively. less refractory.

Instead of using a "pairflof reflux towers as illustrated in Fig. l, aisingledividedjrefiux tower may be used. A reflux, tower. of the type illustrated in Fig. 3, withappropriateconnections-to therest of the still system, for example, may be soused. f

In carrying out the invention, the raw oil supplied to the operation including a dispersed desulphurizing agent,-thatis the raw oil supplied to they operation more objectionable. with respect to' corrosion, isheated to a high temperature while including the dispersed desulphurizing agent in the primary heating zone. By maintaining arelatively high velocity of flow through the primary heating zone, however, deposition within the heating zone of the desulphurizing agent or of reaction'products of desulphurization' or reaction products of any crack reaction products of the desulphurization or of the pracking are not 'permitted'again to pass through either the primary heating zone or the secondary heating zone. Similarly, any excess desulphurizinga entisnot permitted again to pass through, either the primary heating zone or the secondary heating zone. In the vaporizing zone, particularly when a substantial body of liquid is there maintained, further reaction between the oil orthe sulphur compounds of the oil and thedesulphurizing agent may be effected. Lower boiling components of theoil mixture discharged from the primary heating zone may escape atonce to form a part of the distillate product. Higher boiling components of this oil mixture, vaporized in the vaporizing drum, are condensed and returned to the secondary heating zone, so forming part 'iof the circulating still charge. Where the primary heating zone, through which the oil including a dispersed desulphurizing agent ispassed, is'heated by the same stream of heating gases asthe secondary heating zone and where this stream of heating gases passes first in; heat. exchangewith' the oil passing through the" primary heating zone andoil including a dispersed desulphurizing agent is subjected to the most severe conditions maintained in the heating furnace, thus maintaining the raw oil more objectionable with respect to corrosion in intimate contact with the desulphurizing agent used through that part of the still system in which the sulphur compounds present in the oil are most reactive, that is in the region of highest temperature. Corrosion difiiculties seem to be more severe on surfaces in contact with oil vapors than on surfaces in contact with liquid oil, at the same temperature. This invention, however, subjects the raw oil more objectionable with respect to corrosion to intimate contact at high temperature with the desulphurizing agent before this raw oil, or any components of this raw oil, reaches the vapor space in the vaporizing zone. By preheating the raw oil including a dispersed desulphurizing agent, this raw oil is maintained in contact with the desulphurizing agent at elevated temperature for a prolonged period and for a period preceding passage through the primary heating zone. The operation of the invention is intermittent in that the still system must be shutdown for cleaning at more or less regular intervals. A large part of the solid or semi-solid products of the desulp-hurizing reaction and of the cracking reaction, as Well as any excess desulphurizing agent, however, may be discharged in suspension in residual oil discharged through the tar line during regular operation.

Referring to the apparatus illustrated, the vaporizing drum I, the reflux tower 8 or the reflux towers 29 and 3!! or the reflux towers 48 and 49, the connections l8 and I9, and the connections for returning reflux condensates to the heating zones are with advantage lagged or thermally insulated.

In each of the pressure stills illustrated, heat is supplied to both heating zones by the same stream of heating gases. In this respect the apparatus illustrated is a particularly advantageous embodiment of the invention. The heating tubes making up the primary heating zone may, however, be arranged in and heated in a heating furnace separate from the heating furnace in which the heating tubes making up the secondary heating zone are arranged and heated.

The residual oil discharged from the vaporizing zone during operation may be subjected to further distillation for the further separation of oil constituents. This distillation may, for example, be eflected, or in part effected, by reduction of the pressure on the discharged oil.

The character of the desulphurizing agent used permitting, the residue including any unconsumed desulphurizing agent and any heavy products of the desulphurization discharged from the vaporizing zone may be subjected to treatment for recovery of the desulphurizing agent. Where cupriferous desulphurizing agents are used, for example, the residue discharged from the vaporizing zone, either before or after distillation therefrom of lower boiling oil constituents, may be cooled and the cooled residue permitted to settle or subjected to a filtering operation for the separation of the metallic values and this separated material roasted or otherwise treated to.

render it again active to be reused in the process. In general, where lime is used. for example, any unconsumed desulphurizing agent and any heavy products of the desulphurization may be separated from the discharged residue by settling or filtration after cooling.

I claim: i 1. In cracking sulphur-containing hydrocarbon oils by distillation under superatmospheric pressure, the improvement which comprises passing raw oil including-a dispersed desulphurizing agent through a primary heating zoneinto a vaporizing zone in a pressure still, taking ofi vapors from the vaporizing zone Lmder superatmospheric pressure and subjecting them to a refluxing operation, circulating reflux condensate free from suspended matter from the refluxing operation through a secondary heatingzone and thence directly back to the vaporizing zone without permitting circulation of unvaporized oil from the vaporizing zone through the secondary heating zone, heating the oil passing through both heating zones to a cracking temperature, and taking off vapors including vapors of the desired distillate product from the refluxingoperation.

2. In cracking sulphur-containing hydrocarbon oils .by distillation under superatmospheric pressure, the improvement which comprises passing raw oil including a dispersed desulphurizing agent ary heating zone to a cracking temperature and heating the oil passing through the primary heating zone to a temperature not substantially less than that prevailing in the vaporizing zone, and taking ofi vapors including vapors of the desired distillate product from the refluxing operation.

3. In cracking sulphur-containing 'hyrocarbon oils by distillation under superatmospheric pres sure, the improvement which comprises passing raw oil including a dispersed desulphurizing agent through a primary heating zone into a vaporizing zone in a pressure still, taking off vapors from the vaporizing zone under superatmospheric pressure and subjecting them to a refluxing operation, passingraw oil including a dispersed desulphurizing agent on its way to the primary heating zone inindirect heat exchanging relation with the vapors in the refluxing operation, circulating reflux condensate free from suspended matter zone in a pressure still, taking oiT vapors from the vaporizing zone under superatmospheric pressure and subjecting them to two successive refluxing operations, passing reflux condensate free from suspended matter from the first refluxing operation through a secondary heating zone and thence directly back to the vaporizing zone, passing raw oil including a dispersed desulphurizing oilpassing through both heating zones to a crack? agent on its way to the primary heating zone ing temperature, and taking off vapors including in heat exchanging relation with the vapors in vapors of the desired distillate product from the the second refluxing operation and supplying resecond refluxing operation.

flux condensate from the second refluxing oper- V,

ation to the primary heating zone, heating the l V 7 HARRY L. PELZER. 

